CN108328726B - Circulating EGSB reaction device and sewage treatment method based on same - Google Patents
Circulating EGSB reaction device and sewage treatment method based on same Download PDFInfo
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- CN108328726B CN108328726B CN201810069457.6A CN201810069457A CN108328726B CN 108328726 B CN108328726 B CN 108328726B CN 201810069457 A CN201810069457 A CN 201810069457A CN 108328726 B CN108328726 B CN 108328726B
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
Abstract
The invention relates to a circulating EGSB reaction device and a sewage treatment method based on the same, wherein the device comprises a reaction unit, a gas separation unit and a sewage inlet unit, the reaction unit comprises a reactor shell and a sludge collection mechanism arranged in the reactor shell, the gas separation unit comprises a separator which is arranged outside the reactor shell and communicated with the sludge collection mechanism, the bottom of the separator is communicated with the bottom of the reactor shell, the top of the separator is provided with an exhaust port, and the sewage inlet unit is communicated with the separator; during sewage treatment, one part of sewage after denitrification treatment is discharged from the reactor shell, and the other part of sewage is mixed with anaerobic ammonia oxidation sludge and enters the separator through the sludge collection mechanism. Compared with the prior art, the invention realizes the maximized collection of the floating sludge, avoids the aggregation, detention and decay of the high-activity sludge in a non-reaction area, improves the denitrification efficiency of the anaerobic ammonia oxidation sludge and is beneficial to promoting the granulation of the anaerobic ammonia oxidation sludge.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and relates to a circulating EGSB reaction device and a sewage treatment method based on the same.
Background
The discovery of the anaerobic ammonium oxidation bacteria provides a new choice and a new idea for the biological denitrification of the sewage. The anaerobic ammonium oxidation sludge denitrification process of sewage is usually carried out in an anaerobic reactor, the anaerobic reactor which is widely applied is a UASB (upflow anaerobic sludge blanket) reactor, the operation and maintenance of the anaerobic reactor are relatively simple, and the continuous flow operation mode makes the anaerobic reactor more suitable for dealing with continuously generated sewage to be treated. The EGSB (expanded granular sludge bed) reactor is a third-generation anaerobic reactor developed and improved on the basis of the UASB reactor, and is generally recommended at home and abroad due to the characteristics of simple structure, high load, wide adaptability and the like.
However, when the anammox process is operated in the existing EGSB reactor, the anammox bacteria are slowly proliferated, and the amount of nitrogen generated when the nitrogen load is high is large and severe, so that the problem of serious sludge floating is often caused, and further sludge accumulation, putrefaction or loss and the like are caused, thereby affecting the long-term stability of the denitrification performance of the anammox process system. Therefore, the configuration of the anaerobic reactor needs to be designed and optimized aiming at the characteristics of the anaerobic ammonia oxidation sludge, so as to better realize the anaerobic ammonia oxidation denitrification efficiency and promote the application and popularization of the anaerobic ammonia oxidation process.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a circulating EGSB reaction device and a sewage treatment method based on the device.
The purpose of the invention can be realized by the following technical scheme:
the utility model provides a circulating EGSB reaction unit, the device includes reaction unit, gas separation unit and sewage intake unit, the reaction unit include reactor housing and set up the sludge collection mechanism in reactor housing, the gas separation unit including set up reactor housing outside and with the separator that the mechanism is linked together is collected to sludge, the bottom of this separator and the bottom of reactor housing are linked together, the gas vent has been seted up at the top, sewage intake unit and separator be linked together.
Preferably, the separator is a three-phase separator.
Further, the reactor shell comprises a rectification section, a reaction section, an expanding section and a drainage section which are sequentially connected from bottom to top, the bottom of the sludge collection mechanism is positioned in the expanding section, the top of the sludge collection mechanism is communicated with the separator, and the bottom of the separator is communicated with the rectification section.
As a preferable technical scheme, a circulating pump is arranged between the bottom of the separator and the rectifying section.
Furthermore, the reaction section and the drainage section are both vertically arranged in a tubular shape, and the inner diameter of the drainage section is larger than that of the reaction section.
As a preferable technical scheme, the height-diameter ratio of the reactor shell is 25-35, and the height-diameter ratio of the reaction section is 22-28.
As a preferable technical scheme, a plurality of sampling ports are uniformly distributed on the reaction section along the vertical direction.
As a preferred technical scheme, a water outlet of the drainage section is arranged on the drainage section.
Furthermore, the sludge collecting mechanism comprises a sludge collecting cover and a sludge circulating conveying pipe, wherein the bottom of the sludge collecting cover is arranged in the diameter expanding section, and the sludge circulating conveying pipe is arranged between the top of the sludge collecting cover and the separator.
As a preferred technical scheme, the sludge collection cover is immersed in the liquid flow. The sludge collecting cover not only has the functions of maximally collecting floating sludge and gas and shunting partial liquid, but also has the rectification function.
As a preferred technical scheme, the height of the sludge collecting cover is smaller than that of the water outlet of the drainage section.
As a preferable technical scheme, one end of the sludge circulating conveying pipe is communicated with the top of the sludge collecting cover, and the other end of the sludge circulating conveying pipe is communicated with the side surface of the separator.
Further, the rectifying section is funnel-shaped, and the sludge collecting cover is inverted funnel-shaped. The design of the funnel-shaped rectifying section at the bottom of the reactor shell is opposite to the sludge collecting cover with the shape of an inverted funnel at the top, so that a linear flow field structure is formed in the reactor shell by liquid flow.
Further, the gas separation unit further comprises a water seal tank, a gas conveying pipe and an exhaust pipe, one end of the gas conveying pipe is communicated with the exhaust port, the other end of the gas conveying pipe is inserted into the water seal tank, and the exhaust pipe is arranged at the top of the water seal tank and communicated with the inside of the water seal tank.
Furthermore, the sewage inlet unit comprises a sewage tank and a sewage inlet pipe, one end of the sewage inlet pipe is communicated with the sewage tank, and the other end of the sewage inlet pipe is communicated with the top of the separator. The sewage inlet is arranged at the top end of the separator, so that the circulating liquid flow is impacted by the inflow liquid flow, and the hydraulic shearing effect is further enhanced.
As the preferred technical scheme, a sewage inlet pump is arranged on the sewage inlet pipe.
As a preferable technical scheme, the separator adopts an internal spiral design and a water drop operation mode, so that the liquid flow is subjected to a suddenly increased hydraulic shearing action in the three-phase separator.
A sewage treatment method based on the device comprises the following steps: sewage to be treated in the sewage inlet unit enters the reactor shell through the separator and flows from bottom to top in the reactor shell, and meanwhile, anaerobic ammonia oxidation sludge in the reactor shell performs denitrification treatment on the sewage to be treated; one part of the sewage after denitrification treatment is discharged from the reactor shell, and the other part of the sewage is mixed with anaerobic ammonia oxidation sludge, enters the separator through the sludge collecting mechanism and is mixed with the sewage to be treated in the separator; the gas in the separator is discharged through a gas outlet. The sewage mixed with the anaerobic ammonia oxidation sludge enters a separator, the sludge-water mixed liquid and the gas are effectively separated under the action of water drop and the impact of water inflow, the gas enters a water seal tank through a gas conveying pipe, and the sludge-water mixed liquid flows into a circulating pump from the bottom of the separator and circulates again.
Furthermore, in the reactor shell, the concentration of the volatile sludge (MLVSS) of the anaerobic ammonia oxidation sludge is more than or equal to 3000 mg/L.
Furthermore, in the reactor shell, the rising flow velocity of liquid flow is 4-5m/h, the Hydraulic Retention Time (HRT) is 15-20h, and the reaction temperature is 30-35 ℃.
In the invention, flocculent anaerobic ammonium oxidation sludge with relatively small dispersion and density enters the sludge collection mechanism by controlling the ascending flow velocity of the liquid flow, thereby realizing the purpose of sludge recovery; the formation of granular sludge is promoted by creating a reasonable flow field structure. In addition, the specific linear flow state structure in the reactor shell with the larger height-diameter ratio can form a longer circular streamline track, and the effective collision probability among the sludge is increased, so that the granulation of the sludge is promoted, and the granular sludge is formed.
Compared with the prior art, the invention has the following characteristics:
1) the reasonable arrangement of the separator maximizes the hydraulic shearing action, realizes high-efficiency gas removal, and the sludge-water mixed liquid after gas removal can effectively return to the main reaction area in the reaction section in time through the circulating pipeline, thereby avoiding the loss of high-abundance high-activity floating sludge or the aggregation, detention and decay of the floating sludge in a non-reaction area, achieving the purpose of maintaining or increasing the effective working biomass of the system, and effectively improving the denitrification efficiency of the anaerobic ammonium oxidation sludge;
2) the inverted funnel-shaped sludge collecting cover above the reaction section corresponds to the funnel-shaped rectifying section at the bottom of the reaction section and is of a vertically symmetrical structure, an optimized flow field structure can be formed, the granulation process of sludge is facilitated, the collection of floating sludge is maximized, the sludge retention capacity of the device can be effectively improved, and the sludge granulation process is promoted;
3) the collection of the floating sludge is maximized, the aggregation, detention and decay of the high-activity sludge in a non-reaction area are avoided, the denitrification efficiency of the anaerobic ammonia oxidation sludge in the reaction unit is improved, and the granulation of the anaerobic ammonia oxidation sludge is facilitated.
Drawings
FIG. 1 is a schematic view showing the overall structure of a circulating EGSB reaction apparatus in example 1;
FIG. 2 is a Scanning Electron Microscope (SEM) spectrum of anammox granular sludge in the circulating EGSB reactor in example 1, wherein FIG. 2-a shows the outer surface layer of granular sludge, FIG. 2-b shows the outer surface layer EPS of granular sludge, FIG. 2-c shows heterotrophic bacteria growing in the cross section, FIG. 2-d shows the inner surface layer of granular sludge, FIG. 2-e shows heterotrophic bacteria growing in the channels, and FIG. 2-f shows anammox bacteria in the form of spheres;
FIG. 3 is a graph showing a comparison of denitrification efficiencies of the circulating EGSB reactor in example 1 and a conventional EGSB reactor;
the notation in the figure is:
1-exhaust pipe, 2-water seal tank, 3-sewage tank, 4-sewage intake pump, 5-circulating pump, 6-sewage intake pipe, 7-sample connection, 8-sludge collection cover, 9-drainage section delivery port, 10-separator, 11-reactor shell, 1101-rectification section, 1102-reaction section, 1103-expanding section, 1104-drainage section, 12-sludge circulation conveying pipe, 13-gas conveying pipe.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments. The present embodiment is implemented on the premise of the technical solution of the present invention, and a detailed implementation manner and a specific operation process are given, but the scope of the present invention is not limited to the following embodiments.
Example 1:
as shown in fig. 1, the circulating EGSB reaction apparatus comprises a reaction unit, a gas separation unit and a sewage inlet unit, wherein the reaction unit comprises a reactor shell 11 and a sludge collection mechanism disposed in the reactor shell 11, the gas separation unit comprises a separator 10 disposed outside the reactor shell 11 and communicated with the sludge collection mechanism, the bottom of the separator 10 is communicated with the bottom of the reactor shell 11, the top of the separator is provided with an exhaust port, and the sewage inlet unit is communicated with the separator 10.
The reactor shell 11 comprises a rectification section 1101, a reaction section 1102, an expanding section 1103 and a drainage section 1104 which are sequentially connected from bottom to top, the bottom of the sludge collection mechanism is positioned in the expanding section 1103, the top of the sludge collection mechanism is communicated with the separator 10, and the bottom of the separator 10 is communicated with the rectification section 1101. A circulation pump 5 is provided between the bottom of the separator 10 and the rectifying section 1101. The reaction section 1102 and the drainage section 1104 are both vertically arranged in a tubular shape, and the inner diameter of the drainage section 1104 is larger than that of the reaction section 1102. A plurality of sampling ports 7 are uniformly distributed on the reaction section 1102 along the vertical direction. A water outlet 9 of the drainage section is arranged on the drainage section 1104.
The sludge collecting mechanism comprises a sludge collecting cover 8 with the bottom arranged in the diameter expanding section 1103 and a sludge circulating conveying pipe 12 arranged between the top of the sludge collecting cover 8 and the separator 10. The rectifying section 1101 is funnel-shaped, and the sludge collecting cover 8 is inverted funnel-shaped.
The gas separation unit further comprises a water seal tank 2, a gas conveying pipe 13 and an exhaust pipe 1, one end of the gas conveying pipe 13 is communicated with the exhaust port, the other end of the gas conveying pipe 13 is inserted into the water seal tank 2, and the exhaust pipe 1 is arranged at the top of the water seal tank 2 and communicated with the inside of the water seal tank 2.
The sewage inlet unit comprises a sewage tank 3 and a sewage inlet pipe 6, wherein one end of the sewage inlet pipe 6 is communicated with the sewage tank 3, and the other end is communicated with the top of the separator 10. A sewage inlet pump 4 is arranged on the sewage inlet pipe 6. The separator adopts an internal spiral design and a water drop operation mode, so that the liquid flow is subjected to a suddenly increased water conservancy shearing action in the three-phase separator.
The circulating EGSB reactor (MC-EGSB) in this example was operated in conjunction with a conventional EGSB reactor (N-EGSB) and compared. The reaction volumes of the N-EGSB and the MC-EGSB are both 5L, and the height-diameter ratio is both 30. Anaerobic ammonia oxidation sludge is inoculated into MC-EGSB and N-EGSB from a Sequencing Batch Reactor (SBR) mother reactor, and two reaction devices are operated under the condition that control parameters are completely the same: the same starting MLVSS (3000mg/L), the same influent substrate concentration, the same upflow rate (v ═ 4.5m/h), the same hydraulic retention time (HRT ═ 16h), the same operating temperature (31 ℃).
NH during the first 7 days after the operation of the apparatus4 +-N and NO2 --N feed water concentration of about 30 mg/L; after the device operates for 7 days, nitrogen aeration and oxygen removal are carried out on the inlet water, and the denitrification efficiency of the two reaction devices is rapidly improved to about 80 percent; the device is continuously operated for 5 days under the corresponding nitrogen load, and the denitrification efficiency is maintained to be more than 80 percent; then NH in the inlet water4 +-N and NO2 -N was increased to about 60mg/L and the plant was run for a further 45 days under this nitrogen load; then, continuously adding NH in the inlet water4 +-N and NO2 -And the N is increased to about 120mg/L and is operated for about 170 days, and the denitrification performance of the two reaction devices is monitored for about 6 months. Finally, the morphological characteristics of the anaerobic ammonia oxidation granular sludge of the MC-EGSB after long-term operation are characterized by the SEM technology so as to investigate the sludge granulation effect, and the difference of denitrification efficiency of the two reactors after the MC-EGSB is continuously operated for nearly 6 months is analyzed and compared.
The SEM spectrum of the anaerobic ammonia oxidation granular sludge in the MC-EGSB is shown in figure 2, wherein the outer surface layer (figure 2-a and figure 2-b) of the anaerobic ammonia oxidation granular sludge in the MC-EGSB is covered by thick EPS; the inner surface layer (fig. 2-d) is mainly covered by filamentous bacteria and bacilli and contains a small amount of Extracellular Polymer (EPS) of anammox bacteria; the cross section of the granules and the internal and external connecting channels are mainly occupied by spherical anaerobic ammonium oxidation bacteria, and a small amount of filamentous bacteria are proliferated (figure 2-c, figure 2-e and figure 2-f). In the MC-EGSB, the floating sludge or the free anaerobic ammonium oxidation bacteria can return to the main reaction zone in time through the external circulation system, and the part of high-activity floating sludge or the free anaerobic ammonium oxidation bacteria can be attached to and proliferated on the existing sludge particles again after returning to the main reaction zone, or is combined with other sludge flocs in the system and proliferated to form new granular sludge, thereby effectively promoting the granulation process of the anaerobic ammonium oxidation sludge. In addition, as can be seen from FIG. 3, the denitrification efficiency of the two reaction devices was significantly differentiated after 70 days, and finally the denitrification efficiency of the MC-EGSB was significantly better than that of the N-EGSB, which was about 1.25 times that of the N-EGSB. Therefore, the MC-EGSB in the embodiment can obviously improve the denitrification efficiency of the anammox sludge and effectively promote the sludge granulation.
Example 2:
a sewage treatment method based on the circulating EGSB reaction device in the embodiment 1 comprises the following steps: sewage to be treated in the sewage inlet unit enters the reactor shell 11 through the separator 10 and flows from bottom to top in the reactor shell 11, and meanwhile, anaerobic ammonium oxidation sludge in the reactor shell 11 performs denitrification treatment on the sewage to be treated; one part of the sewage after denitrification treatment is discharged from the reactor shell 11, and the other part of the sewage is mixed with anaerobic ammonia oxidation sludge, enters the separator 10 through a sludge collecting mechanism and is mixed with the sewage to be treated in the separator 10; the gas in the separator 10 is discharged through a gas outlet.
Wherein, in the reactor shell 11, the concentration of the volatile sludge of the anaerobic ammonia oxidation sludge is more than or equal to 3000mg/L, the rising flow rate of the liquid flow is 4m/h, the hydraulic retention time is 20h, and the reaction temperature is 30 ℃.
Example 3:
in this example, the reactor shell 11 was set to have a volatile sludge concentration of anammox sludge of 3000mg/L, a flow rate of 5m/h, a hydraulic retention time of 15h, and a reaction temperature of 35 ℃ as in example 2.
Example 4:
in this example, the reactor shell 11 was set to have a volatile sludge concentration of 3500mg/L, a flow rate of 4.5m/h, a hydraulic retention time of 17h, and a reaction temperature of 32 ℃ as in example 2.
The embodiments described above are described to facilitate an understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention based on the disclosure of the present invention.
Claims (6)
1. The circulating EGSB reaction device is characterized by comprising a reaction unit, a gas separation unit and a sewage inlet unit, wherein the reaction unit comprises a reactor shell (11) and a sludge collection mechanism arranged in the reactor shell (11), the gas separation unit comprises a separator (10) which is arranged outside the reactor shell (11) and communicated with the sludge collection mechanism, the bottom of the separator (10) is communicated with the bottom of the reactor shell (11), the top of the separator is provided with an exhaust port, and the sewage inlet unit is communicated with the separator (10);
the reactor shell (11) comprises a rectification section (1101), a reaction section (1102), an expanding section (1103) and a drainage section (1104) which are sequentially connected from bottom to top, the bottom of the sludge collection mechanism is positioned in the expanding section (1103), the top of the sludge collection mechanism is communicated with the separator (10), and the bottom of the separator (10) is communicated with the rectification section (1101);
the sludge collecting mechanism comprises a sludge collecting cover (8) and a sludge circulating conveying pipe (12), wherein the bottom of the sludge collecting cover (8) is arranged in the diameter expanding section (1103), and the sludge circulating conveying pipe (12) is arranged between the top of the sludge collecting cover (8) and the separator (10);
the rectifying section (1101) is funnel-shaped, and the sludge collecting cover (8) is inverted funnel-shaped;
the sewage inlet unit comprises a sewage tank (3) and a sewage inlet pipe (6), one end of the sewage inlet pipe (6) is communicated with the sewage tank (3), and the other end of the sewage inlet pipe is communicated with the top of the separator (10);
the separator (10) adopts an inner spiral design and a water drop operation mode.
2. A cyclic EGSB reaction apparatus according to claim 1, wherein the reaction zone (1102) and the drainage zone (1104) are vertically disposed in a tubular shape, and the inner diameter of the drainage zone (1104) is larger than the inner diameter of the reaction zone (1102).
3. A circulating EGSB reactor apparatus according to claim 1, wherein the gas separation unit further comprises a water seal tank (2), a gas delivery pipe (13), and an exhaust pipe (1), one end of the gas delivery pipe (13) is connected to the exhaust port, the other end is inserted into the water seal tank (2), and the exhaust pipe (1) is disposed on the top of the water seal tank (2) and is connected to the inside of the water seal tank (2).
4. A method for treating wastewater based on the apparatus according to any of claims 1 to 3, characterized in that the method comprises: sewage to be treated in the sewage inlet unit enters the reactor shell (11) through the separator (10) and flows from bottom to top in the reactor shell (11), and meanwhile, anaerobic ammonia oxidation sludge in the reactor shell (11) performs denitrification treatment on the sewage to be treated; one part of the sewage after denitrification treatment is discharged from the reactor shell (11), and the other part of the sewage is mixed with anaerobic ammonia oxidation sludge, enters the separator (10) through the sludge collecting mechanism and is mixed with the sewage to be treated in the separator (10); the gas in the separator (10) is discharged through a gas outlet.
5. The plant-based wastewater treatment method according to claim 4, wherein the reactor shell (11) contains anammox sludge with a volatile sludge concentration of 3000mg/L or more.
6. The plant-based wastewater treatment method according to claim 4, wherein the reactor shell (11) has a flow rate of 4-5m/h, a hydraulic retention time of 15-20h, and a reaction temperature of 30-35 ℃.
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| CN109444001B (en) * | 2018-11-12 | 2023-09-05 | 浙江大学 | Granular sludge bed device and method for observing influence factors of rising water flow velocity |
| CN113184942B (en) * | 2021-06-30 | 2021-09-17 | 苏州湛清环保科技有限公司 | Three-phase separator |
| CN113697941A (en) * | 2021-09-18 | 2021-11-26 | 镇江同源胜环境科技有限公司 | Device for reducing floating sludge of up-flow anaerobic ammonia oxidation reactor |
| CN114436396A (en) * | 2022-01-05 | 2022-05-06 | 安阳工学院 | Anaerobic ammonia oxidation granular sludge stable operation device and anaerobic ammonia oxidation stable operation method |
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| CN201031176Y (en) * | 2007-04-03 | 2008-03-05 | 山东美泉环保科技有限公司 | Circulation type grain sludge reactor |
| CN201473388U (en) * | 2009-05-08 | 2010-05-19 | 王小华 | Secondary floating-prevented sludge circulation device |
| CN104108802B (en) * | 2014-06-12 | 2015-11-18 | 杭州师范大学 | A kind of autotrophic nitrogen removal granule sludge reactor of mud scum automatic pulverizing circulation |
| CN104944578A (en) * | 2015-07-08 | 2015-09-30 | 哈尔滨工业大学 | Method for processing hardly-degradable industrial wastewater adopting mud water double-circulation anaerobic reactor |
| CN105923768B (en) * | 2016-06-08 | 2019-02-12 | 张庆硕 | Ammonia oxidation reactor |
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